KR20100058712A - High efficiency vaporizer and separating method for aldehyde and catalyst using the same - Google Patents

Abstract

PURPOSE: A high efficiency vaporizer, an aldehyde and separation method of a catalyst are provided to improve thermal transfer efficiency of the vaporizer, and to improve efficiency of hydroformylation reaction because of preventing diassembly of ligand and transition metal without activity reduction of the catalyst. CONSTITUTION: A vaporizer(100) comprises the following: a main body(110); an inflow part(10) transferring a mixture to the main body; a plurality of flow control plates(20,21) controlling a flow rate and receiving the mixture of liquid flowing from the inflow part; a heat-exchange tube(40a) in which the mixture of the gas flowed from the inflow part and mixture of the liquid flowing in from the flux controller plate are inserted; a heat exchanger(40) including the heat exchange media(40b) of the high temperature covering the heat-exchange tube; a first exhaust part(50) in which the low viscosity material vaporized in a process of the heat exchange with heat-exchange media through the heat-exchange tube is exhausted; a second exhaust part(60) in which the high viscosity is exhausted among the mixture passing through the heat-exchange tube.

Description

High efficiency vaporizer and separating method for aldehyde and catalyst using the same}

The present invention relates to a vaporizer for separating the aldehyde and catalyst mixture solution according to the hydroformylation reaction of the olefin, more specifically the body; Is formed on one side of the upper body, the inlet port for the mixture of liquid and gaseous phase into the body; A plurality of flow rate adjusting plates for receiving a mixture of liquid phase flowing from the inlet port and adjusting a flow rate; A heat exchanger including a heat exchange tube into which the gaseous mixture introduced from the inlet port and the liquid mixture introduced from the flow rate adjusting unit are injected, and a high temperature heat exchange medium surrounding the heat exchange tube; And a first discharge port formed at one side of the lower part of the main body, and the vaporized low boiling point material discharged through heat exchange with a heat exchange medium while the mixture passes through the heat exchange tube. And a second discharge port formed at a lower portion of the first discharge port, through which the high boiling point material is discharged from the mixture passed through the heat exchange tube.

Hydroformylation reaction, which is generally known as OXO reaction, is a linear (with one carbon number increase in olefin due to the reaction of various olefins and syngas (CO / H ₂ ) in the presence of metal catalysts and ligands). linear, normal) and branched (iso) aldehydes are produced. The oxo reaction was first discovered by Otto Roelen of Germany in 1938, and as of 2001, around 8.4 million tonnes of various aldehydes (including alcohol derivatives) are produced and consumed through the oxo process worldwide ( SRI report , November 2002, 682. 700 A).

Various aldehydes synthesized by the oxo reaction are transformed into aldehyde derivatives acid and alcohol through oxidation or reduction. In addition, after the condensation reaction such as Aldol (Aldol) may be transformed into various acids and alcohols containing a long alkyl group through oxidation or reduction reaction. Such alcohols and acids are used as solvents, additives, and raw materials for various plasticizers.

Currently, metal catalysts used in the oxo process are mainly cobalt (Co) and rhodium (Rh) series, and more than 70% of the world's oxo plants adopt a low pressure OXO process using a rhodium-based catalyst.

In addition to cobalt (Co) and rhodium (Rh), the core metals of the oxo catalyst are iridium (Ir), ruthenium (Ru), osmium (Os), platinum (Pt), palladium (Pd), iron (Fe) and nickel (Ni). ) Can be applied. However, since each metal is known to exhibit catalytic activity in the order of Rh »Co> Ir, Ru> Os> Pt> Pd> Fe> Ni, most of the processes and researches are focused on rhodium and cobalt.

Ligands include phosphine (Phosphine, PR ₃ , R for C ₆ H ₅ , or nC ₄ H ₉ ), phosphine oxide (Phosphine Oxide, O = P (C ₆ H ₅ ) ₃ ), phosphite, Amines, amides or isonitriles are applicable.

Looking at the hydroformylation process in more detail, the olefin is a synthesis gas (CO / H ₂ ) is reacted in the presence of a catalyst to produce normal-aldehyde and iso-aldehyde. After the reaction, products such as aldehydes, unconverted olefins, catalyst mixture solutions and other reaction byproducts are present. This reaction mixture is sent to a separation system to separate the aldehyde and other low boiling materials and catalyst mixture solution. The separated catalyst mixed solution is circulated to the reaction system, the unconverted olefins and syngas in the aldehyde and other low boilers are circulated to the reaction system, and the aldehyde is separated through the normal purification process and the normal- and iso-aldehyde, respectively. Normal-aldehyde is introduced into the aldol condensation reactor to produce aldehydes having an increased carbon number by condensation and dehydration, and then transferred to a hydrogenation reactor, whereby alcohol is produced by hydrogenation. The reactant at the outlet of the hydrogenation reactor produces an alcohol product after separation.

Referring to the separation process of the aldehyde and catalyst mixed solution in the hydroformylation process with reference to the vaporizer shown in Figure 1 attached as follows. The reaction mixture after reacting the olefin and syngas (CO / H ₂ ) in the presence of the catalyst mixture solution is introduced through the inlet port (1) of the vaporizer, and the liquid mixture in the reaction mixture is passed through the dispersion plate (2). It is injected into the heat exchange tube (4). The gaseous mixture in the reaction mixture is injected into the heat exchange tube 4 through a gas pipe 3 mounted on the dispersion plate 2. Passing through the heat exchange tube 4, the low boiling point component of the reaction mixture is evaporated and removed from the vaporizer in the vapor state, and the high boiling point component moves to the bottom of the vaporizer and is discharged and then circulated to the reactor. At this time, aldehydes, unconverted olefins, and the like, which are present in the reaction mixture, are removed from the vaporizer as a low boiling point material, partly circulated to the reaction system, and partly recovered to the target material through purification. The catalyst mixture solution separated in the vaporizer is circulated to the reactor as a high boiling point material.

In the course of introducing the reaction mixture, the liquid reaction mixture is accommodated in the dispersion plate 2 and then injected into the heat exchange tube 4, which generates a gradient in the acceptance process in the dispersion plate, and thus is injected into the heat exchange tube 4. Since the amount of liquid phase is not uniform, there is a problem that the heat exchange efficiency falls. In addition, the flow of the gaseous reaction mixture injected into the heat exchange tube 4 through the gas pipe 3 serves as another cause of the uniformity of the amount of the liquid phase injected into the heat exchange tube 4. If the heat exchange efficiency is low, the activity of the temperature sensitive catalyst is reduced. In addition, when the aldehyde to be separated is an aldehyde having a high boiling point (aldehyde having 6 or more carbon atoms), there is a problem in that the transition metal and the ligand are decomposed. Deactivation of such catalysts and degradation of ligands lower the function of the circulating catalysts, thereby reducing the reaction efficiency.

In order to solve the problems of the prior art as described above, an object of the present invention is to provide a vaporizer having a high heat transfer efficiency by uniformly injecting the reaction mixture of liquid and gas phase into the heat exchange tube.

The above and other objects of the present invention can be achieved by the present invention described below.

In order to achieve the above object, the present invention

main body; Is formed on one side of the upper body, the inlet port for the mixture of liquid and gaseous phase into the body; A plurality of flow rate adjusting plates for receiving a mixture of liquid phase flowing from the inlet port and adjusting a flow rate; A heat exchanger including a heat exchange tube into which the gaseous mixture introduced from the inlet port and the liquid mixture introduced from the flow rate adjusting unit are injected, and a high temperature heat exchange medium surrounding the heat exchange tube; And a first discharge port formed at one side of the lower part of the main body, and the vaporized low boiling point material discharged through heat exchange with a heat exchange medium while the mixture passes through the heat exchange tube. And a second discharge port formed at a lower portion of the first discharge port and discharging a high boiling point material from the mixture passed through the heat exchange tube.

The plurality of flow control plates are each plate is arranged at a predetermined interval, the head of the liquid mixture is preferably formed in each plate 20 mm to 200 mm, the diameter of the flow control port of the upper plate d1, lower In view of the diameter of the flow control port of the plate as d2, the ratio d1 / d2 is preferably in the range of 1 to 3.

The heat exchanger preferably comprises means for circulating the heat exchange medium.

The liquid and gaseous mixture is a reaction mixture containing aldehyde, unconverted olefin, and catalyst mixed solution by hydroformylation reaction of olefin, low boiling point material is aldehyde, unconverted olefin, high boiling point material is catalyst mixed solution Is preferably.

The vaporizer includes a gas pipe for injecting a mixture of gaseous phase flowing into the body through the inlet port into the heat exchange tube, the gas pipe is matched 1: 1 with the heat exchange tube, the lower end of the gas pipe at a predetermined interval to the heat exchange tube It is preferable that it is inserted.

The diameter of the gas pipe is preferably 30 to 55% of the diameter of the heat exchange tube.

As another means for solving the above problems, the present invention provides a liquid phase containing aldehyde, unconverted olefin, and catalyst mixed solution produced by the reaction of olefin and syngas (CO / H ₂ ) in the presence of a catalyst mixed solution. And introducing a gaseous reaction mixture into an inlet port of the vaporizer; Adjusting the amount of the introduced reaction mixture and injecting it into a heat exchange tube; And in the course of passing through the heat exchange tube, separating and discharging the vaporized aldehyde and unconverted olefin and the catalyst mixed solution through heat exchange with a heat exchange medium, respectively.

The olefin is ethylene, propylene, butene, 1-hexene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene, 1-eicosene, 2-butene, 2-methylpropene, 2-pentene, 2-hexene, 2-heptene, 2-ethylhexene, 2-octene , Styrene, 3-phenyl-1-propene or 4-isopropylstyrene, the catalyst mixture solution preferably includes a transition metal catalyst and a ligand, and the solvent of the catalyst mixture solution is an aldehyde or an alcohol. It is preferable.

As described above, the vaporizer according to the present invention is uniformly injected with the liquid and gaseous mixture into the heat exchange tube by a gas pipe in which a plurality of flow control plate and the heat exchange tube is 1: 1 matched, accordingly the heat transfer of the vaporizer The efficiency is improved. In the hydroformylation process of an olefin, when the aldehyde and catalyst mixed solution is separated using such a vaporizer, the decomposition of transition metals and ligands can be prevented without lowering the activity of the catalyst, thereby improving the efficiency of the hydroformylation reaction. do.

EMBODIMENT OF THE INVENTION Hereinafter, this invention is demonstrated in detail.

Hydroformylation is a process for preparing aldehydes by reacting olefins and syngas (CO / H ₂ ) in the presence of a catalyst.

The accompanying Figure 2 schematically shows a hydroformylation process, referring to this.

Injecting olefin and syngas (CO / H ₂ ) into the reactor (A) in which the catalyst mixture solution is present (a). After the reaction, there is a reaction mixture in the reactor containing the product aldehyde, unconverted olefin, syngas, catalyst mixture solution and other reaction by-products, the reaction mixture is introduced into the vaporizer (b) (b). At this time, the dissolved gas dissolved in the catalyst mixed solution in the reactor is reduced in pressure in the process of flowing into the vaporizer, and flows into the inlet port of the vaporizer in the gas phase. The liquid and gaseous reaction mixture entering the vaporizer is separated by a heat exchange device in the vaporizer into a catalyst mixture solution which is an aldehyde and other low boiling point substances and a high boiling point substance. The separated catalyst mixed solution is circulated to the reaction system (c), and low boiling point aldehydes, unconverted olefins, syngas and the like are vaporized and recovered in a vapor state (d). The recovered low boiling point material is separated separately from normal- and iso-aldehyde through separate purification processes, and the normal-aldehyde can be used for producing alcohol by aldol condensation and hydrogenation.

The present invention relates to a vaporizer for separating the catalyst mixture solution and aldehyde after the reaction of the olefin and syngas (CO / H ₂ ), the liquid and gaseous reaction mixture is uniformly injected into the heat exchange tube heat transfer efficiency It is characterized by high.

Hereinafter, a vaporizer according to an embodiment of the present invention will be described in detail with reference to the accompanying drawings.

3 is a cross-sectional view of a vaporizer according to an embodiment of the present invention.

Vaporizer 100 according to an embodiment of the present invention the main body 110; An inlet port 10 formed at one side of the main body 110 and into which a mixture of liquid and gaseous phase is introduced into the main body; A plurality of flow control plates (20, 21) for receiving a mixture of the liquid flowing from the inlet port and adjusting the flow rate; A heat exchanger including a heat exchange tube 40a into which the gaseous mixture introduced from the inlet port and the liquid mixture introduced from the flow regulating plate are injected, and a high temperature heat exchange medium 40b surrounding the heat exchange tube ( 40); And a first discharge port 50 formed at one side of the lower portion of the main body 110 and discharging the low boiling point material vaporized through heat exchange with a heat exchange medium in the course of passing the mixture through the heat exchange tube 40a. And a second discharge port 60 formed below the first discharge port and discharging the mixture passing through the heat exchange tube. It includes.

A mixture of liquid and gaseous phase is introduced into the main body through the inlet port 10 formed at one side of the main body 110. The liquid mixture introduced into the main body is accommodated in the plurality of flow control plates 20 and 21, and the flow rate is adjusted and transferred to the heat exchange tube 40a. The plurality of flow control plates (20, 21) are each plate is arranged at a predetermined interval, each plate should be formed of the head of the liquid mixture 20mm to 200mm, if the head is less than 20mm liquid mixture As the gas phase mixture flows in through this flowing port, the gas phase and liquid mixture are separated and cannot be uniformly delivered to the heat exchange tube inlet. When the flow rate adjustment port diameter of the upper plate is d1 and the flow rate adjustment port diameter of the lower plate is d2, the ratio d1 / d2 is preferably 1 to 3. When the ratio of d1 / d2 is less than 1, the liquid mixture head is not formed on the lower plate. When the ratio exceeds 3, the liquid mixture head is not formed on the upper plate, and the head of the liquid mixture on the lower plate increases the separation efficiency. This can be reduced.

The number of flow rate control plates may be determined according to the amount of raw material supplied to the vaporizer and the ratio of gaseous phase and liquid phase contained in the raw material, but is not limited thereto, but is preferably 2 to 4, more preferably two.

The liquid mixture introduced into the main body is first received in the first plate 20 and then discharged by the flow control port 20a formed in the first plate and received in the second plate 21 before being transferred to the heat exchange tube. That is, the flow rate is controlled by the plurality of plates to transfer the liquid mixture to the heat exchange tube. The conventional vaporizer has a problem that the gradient is generated in the mixture of the liquid phase accommodated in the flow rate control plate is not uniform amount injected into the heat exchange tube. However, the vaporizer according to the present invention is accommodated in the second plate 21 while the flow rate is controlled by the flow rate adjustment port 20a formed in the first plate even if a gradient occurs in the liquid mixture contained in the first plate, the heat exchange The amount of liquid mixture delivered to the tube is made uniform.

After the hydroformylation reaction in which olefins and syngas (CO / H ₂ ) are reacted in the presence of a catalyst mixed solution, a reaction mixture containing aldehydes, unconverted olefins, syngas, catalyst mixed solutions and other reaction by-products as target substances is prepared. It flows into the main body 110 through the inlet port 10. At this time, dissolved gas, such as unconverted olefin and synthesis gas, dissolved in the catalyst mixed solution in the reactor is lowered in the process of flowing into the vaporizer and flows into the inlet port of the vaporizer in the gas phase. The reactor in which the hydroformylation reaction proceeds is maintained at a pressure of 10 bar to 30 bar at a temperature of 70 to 100 degrees, and the vaporizer for separating the catalyst and the aldehyde is maintained at a pressure of 0 bar to 2 bar at a temperature of 100 to 130 degrees. It is desirable to be.

The mixture of the gaseous phase flowing from the inlet port and the liquid phase flowing from the flow rate control unit is injected into the heat exchange tube 40a.

The heat exchange tube 40a is surrounded by a high temperature heat exchange medium 40b, which heat exchanges between the mixture passing through the heat exchange tube 40a and the heat exchange medium 40b to form a low boiling point material in the mixture. Vaporize. The heat exchange medium 40b is preferably maintained at a higher temperature than the mixture passing through the heat exchange tube 40a. As the mixture passes through the heat exchange tube 40a, the low boiling point material undergoes heat exchange with the heat exchange medium 40b to vaporize.

The heat exchanger 40 comprising the heat exchange tube 40 and the hot heat exchange medium 40b surrounding it may comprise circulation means 70 for circulating the heat exchange medium 40b. The circulation means 70 increases the temperature of the heat exchange medium 40b whose temperature has fallen through the heat exchange process, and then circulates the heat exchange unit.

In the course of the hydroformylation reaction of the liquid and gaseous reaction mixture passing through the heat exchange tube, low-boiling aldehydes, unconverted olefins, syngas and the like are vaporized through heat exchange with a heat exchange medium. It is preferable that the boiling point of aldehyde, unconverted olefin, syngas, etc. is 80 degrees C or less, and the heat exchange medium 40b is maintained at 120-150 degreeC.

In the course of passing the mixture through the heat exchange tube 40a, the low boiling point material vaporized through heat exchange with the heat exchange medium 40b is discharged through the first discharge port 50 formed at one side of the lower part of the main body in a vapor state. . The unboiled high boiling point material in the mixture passing through the heat exchange tube 40a is discharged through the second discharge port 60. The first discharge port 50 is a port through which vaporized low-boiling materials are discharged in a vapor state, and the second discharge port 60 is a port through which high-boiling substances that are not vaporized are discharged in the liquid phase. ) Is formed below the first discharge port 50.

When the reaction mixture by the hydroformylation reaction is introduced into the inlet port of the vaporizer, vaporized aldehydes, unconverted olefins, syngas, etc. during the passage of the heat exchange tube are vaporized through the first outlet port 50. It is discharged and can be used separately from the normal- and iso-aldehydes via separate purification processes. The catalyst mixture solution, which is a high boiling point material in the reaction mixture, may be discharged through the second discharge port 60 and circulated to the reaction system.

As described above, the vaporizer according to the present invention has high heat transfer efficiency, and thus the catalyst is not exposed to high temperature for a long time, so that the activity of the catalyst is not lowered, and the decomposition of the catalyst and ligand can be prevented, so that the function of the circulated catalyst is lowered. Instead, the efficiency of the hydroformylation reaction is increased.

The vaporizer preferably includes a gas pipe 30 for injecting a gaseous mixture introduced into the body 110 through the inlet port 10 into the heat exchange tube. The gas pipe 30 is matched 1: 1 with the heat exchange tube 40a, and the lower end of the gas pipe 30 is inserted into the heat exchange tube at predetermined intervals D and D '.

4 is an enlarged cross-sectional view of the matching portion of the gas pipe 30 and the heat exchange tube 40a.

The diameters of the heat exchange tube 40a and the gas pipe 30 are determined according to the target material to be separated, but the diameter of the gas pipe is 30 to 55% of the diameter of the heat exchange tube D ', and is inserted into the heat exchange tube 40a. Preferably, the length of the lower end of the gas pipe 30 is 30 to 80% of the heat exchange tube diameter D '.

Specifically, the diameter of the heat exchange tube 40a is preferably 20 to 25 mm, and the diameter of the gas pipe 30 is preferably 8 to 10 mm. In addition, the length of the lower end of the gas pipe 30 inserted into the heat exchange tube 40a is preferably 10 to 15 mm. The gas pipe 30 and the heat exchange tube 40a may be provided in plural numbers according to the amount of the raw material supplied to the vaporizer, but the present invention is not limited thereto, and 600 to 700 pieces may be provided.

As described above, the vaporizer according to the present invention, the flow rate is controlled by a plurality of plates, not only the amount of the mixture of the liquid to be transferred to the heat exchange tube is uniform, but also the mixture of the gas phase injected by the gas pipe 30 The amount of is uniform. In addition, although the flow of the liquid phase is hindered by the flow of the gas phase injected into the heat exchange tube, the vaporizer according to the present invention has been improved such a problem. Therefore, the amount of the mixture flowing through the heat exchange tube is uniform, so that the efficiency of the vaporizer is excellent.

The invention also

Introducing a liquid and gaseous reaction mixture including aldehyde, unconverted olefin, and catalyst mixture solution, produced by the reaction of olefins and syngas (CO / H ₂ ) in the presence of a catalyst mixture solution, into the inlet port of the vaporizer ;

Adjusting the amount of the introduced reaction mixture and injecting it into a heat exchange tube; And

In the process of passing through the heat exchange tube, and separating and discharging the aldehyde and unconverted olefin and the catalyst mixture solution, respectively, through heat exchange with the heat exchange medium.

The olefin used in the hydroformylation reaction is not limited thereto, and may be an olefin having 2 to 20 carbon atoms, and more specifically, ethylene, propylene, butene, 1-hexene, 1-octene, 1-nonene, and 1- Decene, 1-undecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene, 1-eicosene, 2-butene , 2-methylpropene, 2-pentene, 2-hexene, 2-heptene, 2-ethylhexene, 2-octene, styrene, 3-phenyl-1-propene or 4-isopropylstyrene; It is more preferable that it is propylene or butene.

In addition, the catalyst mixed solution may include a transition metal catalyst and a ligand. The transition metal catalyst can be used without limitation as long as it is generally used in the art, for example, cobalt (Co), rhodium (Rh), iridium (Ir), ruthenium (Ru), osmium (Os), platinum (Pt) Or a catalyst having a transition metal such as palladium (Pd), iron (Fe), or nickel (Ni) as the center metal. Specifically, cobalt carbonyl [Co ₂ (CO) ₈ ], acetylacetonatodicarbonyldium [Rh (AcAc) (CO) ₂ ], acetylacetonatocarbonyltriphenylphosphinedium [Rh (AcAc) ( CO) (TPP)], hydridocarbonyltri (triphenylphosphine) rhodium [HRh (CO) (TPP) ₃ ], acetylacetonatodicarbonyliridium [Ir (AcAc) (CO) ₂ ] and hydrido One or more complex catalysts selected from the group consisting of carbonyltri (triphenylphosphine) iridium [HIr (CO) (TPP) ₃ ] can be used.

The ligand may be a trisubstituted phosphine (Phosphine), phosphine oxide (Phosphine Oxide), amines (Amine), amides (Amide), or isonitrile (Isonitrile), and the use of trisubstituted phosphine desirable. Trisubstituted phosphines include, but are not limited to, triaryl phosphine, triaryl phosphite, alkyldiaryl phosphine and the like, more specifically triphenylphosphine, tritolylphosphine, triphenylphosphite and n -Butyl diphenyl phosphine, etc. can be used.

Controlling the amount of the introduced reaction mixture and injecting it into the heat exchange tube can be achieved through a vaporizer according to the present invention.

The vaporizer according to the present invention is excellent in heat transfer efficiency, the catalyst is not exposed to high temperature for a long time, the activity degradation of the catalyst and decomposition of the catalyst and ligand does not occur, the reaction efficiency is improved. In addition, when the target material to be separated after the hydroformylation reaction is an aldehyde having a high boiling point (for example, an aldehyde having 6 or more carbon atoms), the temperature of the heat medium of the vaporizer is increased, thereby lowering the activity of the catalyst and Decomposition may occur, but it may be prevented when using the vaporizer according to the present invention.

The invention is explained in more detail through the following examples. However, these embodiments are merely exemplary and do not limit the technical scope of the present invention.

EXAMPLE

Example 1

Using a carburetor of the type shown in FIG. 3 with two flow control plates, the reaction product of 46.7 ton / hr was constantly supplied to the inlet of the vaporizer while the vaporizer temperature was continuously operated at 116.5 degrees and the pressure was 1.61 bar. Low-boiling substances such as unconverted olefins and synthesis gas were separated at 29.6 ton / hr, and high-boiling substances as catalyst mixture solutions were separated at 13.7 ton / hr. No catalyst loss to the top of the vaporizer was observed during the separation, and the catalysts that participated in the reaction were able to recover the entire amount of the catalyst mixture and recycle to the reactor.

In this case, the relative ratio of the low boiling point material separation amount and the high boiling point material separation amount was 2.4, which means that it is possible to effectively separate the low boiling point aldehyde and the high boiling point catalyst.

Comparative Example 1

Using a carburetor of the same type as shown in FIG. 1 with one flow regulating plate, a constant supply of 36.2 ton / hr of reaction product was carried out at the inlet of the vaporizer while the vaporizer temperature was continuously operated at 117.5 degrees and the pressure was 1.6 bar. Low-boiling substances such as unconverted olefins and syngas were 23.4 ton / hr, and high-boiling substances as catalyst mixture solutions were separated into 12.8 ton / hr.

The relative ratio of the separation of low-boiling substances and that of high-boiling substances was 1.8.

As described above, in the case of the embodiment using a high-efficiency vaporizer having a two-stage flow control plate, the ratio of the separation of low boiling point material and high boiling point material was relatively higher than that of Comparative Example 1. This means that according to the invention, the same energy can be used to effectively remove larger amounts of low boiling materials, ie reaction products, from the catalyst.

In addition, it is possible to lower the separation temperature of the vaporizer can be expected a secondary effect to protect the temperature-sensitive reaction catalyst.

Although the present invention has been described in detail with reference to the described embodiments, it will be apparent to those skilled in the art that various modifications and variations are possible within the scope and spirit of the present invention, and such modifications and modifications fall within the scope of the appended claims. It is also natural.

1 is a cross-sectional view of a vaporizer used in the prior art.

Figure 2 schematically shows a process diagram of hydroformylation of olefins.

3 is a cross-sectional view of a carburetor according to an embodiment of the present invention, the lower right portion is shown in more detail the lower end of the carburetor.

4 is an enlarged cross-sectional view of a gas pipe and a heat exchange tube of a vaporizer according to an embodiment of the present invention.

<Explanation of symbols for the main parts of the drawings>

1: inlet port 2: dispersion plate

3: gas pipe 4: heat exchange tube

100: carburetor 110: carburetor body

10: inlet port 20, 21: flow rate control plate

30: gas pipe 40: heat exchange part

40a: heat exchange tube 40b: heat exchange medium

50: first discharge port 60: second discharge port

70: circulation

Claims (9)

main body; Is formed on one side of the upper body, the inlet port for the mixture of liquid and gaseous phase into the body; A plurality of flow rate adjusting plates for receiving a mixture of liquid phase flowing from the inlet port and adjusting a flow rate; A heat exchanger including a heat exchange tube into which the gaseous mixture introduced from the inlet port and the liquid mixture introduced from the flow rate adjusting unit are injected, and a high temperature heat exchange medium surrounding the heat exchange tube; And A first discharge port formed at one side of the lower part of the main body, and the vaporized low boiling point material is discharged through heat exchange with a heat exchange medium while the mixture passes through a heat exchange tube; And  And a second discharge port formed under the first discharge port and discharging a high boiling point material from the mixture passed through the heat exchange tube. The method of claim 1, The plurality of flow control plate is a vaporizer, characterized in that each plate is arranged at a predetermined interval, each plate has a head of the liquid mixture of 20 mm to 200 mm. The method of claim 1, Wherein said heat exchanger comprises means for circulating a heat exchange medium. The method of claim 1, The mixture of liquid and gaseous phase is a reaction mixture containing aldehyde, unconverted olefin, and catalyst mixed solution by hydroformylation reaction of olefin, low boiling point material is aldehyde, unconverted olefin, and high boiling point material is catalyst mixed solution. Carburetor, characterized in that. The method of claim 1, And a gas pipe for injecting a gaseous mixture introduced into the main body through the inlet port into a heat exchange tube, wherein the gas pipe is matched 1: 1 with the heat exchange tube, and a lower end of the gas pipe is inserted at a predetermined interval into the heat exchange tube. Carburetor, characterized in that. The method of claim 5, The diameter of the gas pipe is a vaporizer, characterized in that 30 to 50% of the diameter of the heat exchange tube. Introducing a liquid and gaseous reaction mixture including aldehyde, unconverted olefin, and catalyst mixture solution, produced by the reaction of olefins and syngas (CO / H ₂ ) in the presence of a catalyst mixture solution, into the inlet port of the vaporizer ; Adjusting the amount of the introduced reaction mixture and injecting it into a heat exchange tube; And In the process of passing through the heat exchange tube, separating and discharging the aldehyde and unconverted olefin and the catalyst mixed solution vaporized through heat exchange with the heat exchange medium, respectively. The method of claim 7, wherein The olefin may be ethylene, propylene, butene, 1-hexene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene, 1-eicosene, 2-butene, 2-methylpropene, 2-pentene, 2-hexene, 2-heptene, 2-ethylhexene, 2-octene , Styrene, 3-phenyl-1-propene or 4-isopropylstyrene. The method of claim 7, wherein The catalyst mixture solution is a separation method of the aldehyde and catalyst, characterized in that it comprises a transition metal catalyst and a ligand.

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